WO1986006710A1 - Procede et dispositif d'oxydation a l'aide d'un procede a l'anthraquinone pour la fabrication de peroxyde d'hydrogene - Google Patents

Procede et dispositif d'oxydation a l'aide d'un procede a l'anthraquinone pour la fabrication de peroxyde d'hydrogene Download PDF

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Publication number
WO1986006710A1
WO1986006710A1 PCT/AT1986/000039 AT8600039W WO8606710A1 WO 1986006710 A1 WO1986006710 A1 WO 1986006710A1 AT 8600039 W AT8600039 W AT 8600039W WO 8606710 A1 WO8606710 A1 WO 8606710A1
Authority
WO
WIPO (PCT)
Prior art keywords
working solution
gas
reactor
coalescence
oxidizing gas
Prior art date
Application number
PCT/AT1986/000039
Other languages
German (de)
English (en)
Inventor
Jörg KEMNADE
Bernhard Maurer
Original Assignee
Österreichische Chemische Werke Gesellschaft M.B.H
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Österreichische Chemische Werke Gesellschaft M.B.H filed Critical Österreichische Chemische Werke Gesellschaft M.B.H
Priority to AT86902766T priority Critical patent/ATE47819T1/de
Priority to DE8686902766T priority patent/DE3666797D1/de
Publication of WO1986006710A1 publication Critical patent/WO1986006710A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B15/00—Peroxides; Peroxyhydrates; Peroxyacids or salts thereof; Superoxides; Ozonides
    • C01B15/01—Hydrogen peroxide
    • C01B15/022—Preparation from organic compounds
    • C01B15/023—Preparation from organic compounds by the alkyl-anthraquinone process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00168—Controlling or regulating processes controlling the viscosity

Definitions

  • the object of the invention is therefore to carry out the oxidation of the hydrogenated working solution with an oxygen-containing gas in a shorter time and with less technical effort than in the previously known processes, with the greatest possible protection of the working solution itself.
  • coalescence-inhibited system which has a gas content of at least 40 percent by volume, preferably 50 to 60 percent by volume, and in which the average size of the gas bubbles has a diameter of at most 2.5 mm, preferably below 1, 5 mm, whereupon this coalescence-inhibited system is introduced directly or via a distributor element into the lower part of a tubular, preferably built-in, reactor which is dimensioned such that in it the most complete possible conversion of the oxygen with that present in the hydrogenated working solution Hydroquinone is possible, after which the fully oxidized mixture of hydrogenated working solution and oxidizing gas is separated in a known manner into gas and liquid.
  • Systems known to be coalesced are known to be those in which the existing gas bubbles - if there is no external influence on the system - maintain their size.
  • the liquids are characterized by certain values that influence the interface, e.g. Toughness and specific surface tension, from.
  • a simple preliminary test can be used to determine whether or not a liquid can form a coalescence-inhibited system with the gas in question.
  • sieve plates or frits For the production of gas bubbles with an average diameter of at most 2.5 mm, but preferably less than 1.5 mm, sieve plates or frits, the openings of which are adapted in size to the desired bubble diameter, can be used.
  • a device known per se has proven to be particularly suitable, which consists of a tube whose initial nominal pipe diameter narrows to a throat and then reaches the same or a different nominal diameter again. These types of devices cause little pressure loss.
  • the hydrogenated working solution and the oxidizing gas are introduced into this device either together or separately, but then in cocurrent on the side facing the hydrogenation stage.
  • the mixture of working solution and gas begins before it enters the throat.
  • the intensive mixing is achieved by flowing through the throat.
  • a coalescence-inhibited system is created with a narrow spectrum of the diameter of the gas bubbles. The size of the throat has an influence on this spectrum depending on the volume flow.
  • the bubble diameter depends on the energy input and this in turn depends on the pressure loss and the volume throughput.
  • the required pressure loss for a given throughput is determined by the choice of the nominal throat size.
  • the bubble diameter is generally approx. 0.5 mm.
  • oxygen-nitrogen mixtures can be used as oxidizing gases, including pure oxygen. However, air is preferably used.
  • the coalescence-inhibited system of hydrogenated working solution and oxidizing gas obtained according to the invention is introduced into a tubular reactor via a distributor element.
  • the mixing element for its production can be attached to this reactor directly at the bottom or in the vicinity of the bottom in the side wall; however, it can also be arranged standing or lying separately from the reactor and connected to it by a line.
  • the coalescence-inhibited system enters the lower part of the reactor, possibly via a distributor.
  • This distributor preferably in the form of a ring, is constructed in such a way that it uniformly applies the mixture of hydrogenated working solution and oxidizing gas to the cross section of the reactor.
  • "distributor” is not to be understood to mean any single organs which can have a coalescing effect on the gas bubbles, such as e.g. Sieve trays.
  • the openings of the distributor must therefore be dimensioned and arranged so that the mixture is not distributed over the reactor cross-section, but evenly even at high throughput.
  • the tubular reactor itself is free of any internals in its reaction space, except for the distributor if necessary. empty.
  • the reactor is dimensioned such that the degree of oxidation, based on the hydroquinone present, is at least 90%, but preferably at least 98%, is before the gas-containing working solution enters a liquid-gas separator. It was found that a reaction space of 8 to 30 m in height within the reactor met the above requirement.
  • the oxidation reaction itself takes place at pressures from 1 to almost 15 bar, preferably at 2 to 5 bar.
  • the most suitable temperatures are 30 to 80 ° C.
  • the working solution and residual gas which when using Nitrogen-oxygen mixtures, especially of air, mainly consisting of the non-reactive nitrogen, a liquid-gas separator which is conventional per se, e.g. a centrifugal separator, and separated from one another in a manner known per se.
  • a liquid-gas separator which is conventional per se, e.g. a centrifugal separator, and separated from one another in a manner known per se.
  • This gas separator can be located in the upper part of the reactor following the actual reaction space or outside the reactor and can be connected to it by a line.
  • the separated gas can be disposed of via an activated carbon unit.
  • the oxidized working solution is passed on for extraction.
  • FIG. 1 shows the mixing element used according to the invention.
  • 2 shows the various possible combinations of mixing element according to the invention, Distributor and reactor.
  • 3 presents the oxidation tower known from DE-AS 20 03 268 and
  • FIG. 4 shows a device which is particularly suitable for carrying out the method according to the invention.
  • the hydrogenated working solution (AL) are introduced into the mixing element 1 via line 2 and the oxidizing gas at 4 via line 3.
  • the gas-liquid mixture After flowing through the upper part of the mixing element 1, the gas-liquid mixture enters the throat 5, where a particularly intensive mixing and division of the gas into bubbles with a diameter of at most 2.5 mm, preferably much smaller, takes place.
  • the very large exchange surface required for the oxidation is created here, in a coalescence-inhibited system. This coalescence-inhibited mixture is now in the empty reactor
  • the large exchange area means that the reaction rate is greatly increased, so that at least the same degrees of oxidation as before, if not higher, up to practically 100% can be achieved, and this in a shorter residence time mixture to be oxidized than before.
  • the oxi dation reactors can thus be designed smaller, because the apparatus yield is increased and because volume-intensive internals, such as packing, are superfluous. At the same time, the quantities of by-products and degradation products are reduced to a minimum, ie the working solution is spared.
  • the cross-sectional load for working solution is therefore approximately 31 cubic meters / m 2 h and for air 1440 normal cubic meters / m 2 h.
  • the space-time yield amounts to

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

Pour pouvoir exécuter l'oxydation en circuit fermé dans la fabrication de peroxyde d'hydrogène en utilisant le procédé à l'anthraquinone, selon lequel on fait passer un gaz oxydant sur une solution hydrogénée dans un réacteur à courants parallèles à une température en dessous de 100oC, à une pression inférieure à 15 bar et en augmentant la vitesse de réaction dans l'étape d'oxydation, on mélange intensivement la solution hydrogénée après l'étape d'hydrogénation avec un gaz oxydant sous formation d'un système inhibant la coalescence et on introduit le tout dans la partie inférieure largement dégagée de tout obstacle d'un réacteur, dans lequel il se produit une réaction presque totale de l'oxygène avec l'hydroquinone présente dans la solution hydrogénée. Le dispositif pour la mise en oeuvre du procédé comprend un mélangeur (1), un réacteur (6) à partie inférieure dégagée et, si nécessaire, un distributeur (7).
PCT/AT1986/000039 1985-05-07 1986-05-06 Procede et dispositif d'oxydation a l'aide d'un procede a l'anthraquinone pour la fabrication de peroxyde d'hydrogene WO1986006710A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AT86902766T ATE47819T1 (de) 1985-05-07 1986-05-06 Verfahren und vorrichtung zur durchfuehrung der oxidation im anthrachinonverfahren zur herstellung von wasserstoffperoxid.
DE8686902766T DE3666797D1 (en) 1985-05-07 1986-05-06 Oxidation method and device by means of an anthraquinone process for producing hydrogen peroxyde

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT136185 1985-05-07
ATA1361/85 1985-05-07

Publications (1)

Publication Number Publication Date
WO1986006710A1 true WO1986006710A1 (fr) 1986-11-20

Family

ID=3512223

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AT1986/000039 WO1986006710A1 (fr) 1985-05-07 1986-05-06 Procede et dispositif d'oxydation a l'aide d'un procede a l'anthraquinone pour la fabrication de peroxyde d'hydrogene

Country Status (10)

Country Link
EP (1) EP0221931B1 (fr)
JP (1) JPS62502821A (fr)
AR (1) AR240549A1 (fr)
AT (1) ATE47819T1 (fr)
AU (1) AU587257B2 (fr)
CA (1) CA1283273C (fr)
DE (1) DE3666797D1 (fr)
IN (1) IN168293B (fr)
WO (1) WO1986006710A1 (fr)
ZA (1) ZA863259B (fr)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2652344A1 (fr) * 1989-09-22 1991-03-29 Kemira Oy Procede pour la production de peroxyde d'hydrogene.
FR2730987A1 (fr) * 1995-02-28 1996-08-30 Chemoxal Sa Installation de production d'eau oxygenee sur le site d'une papeterie
WO2002034668A1 (fr) * 2000-10-21 2002-05-02 Degussa Ag Procede continu d'hydrogenation
EP1209122A1 (fr) * 2000-11-24 2002-05-29 Degussa AG Procédé d' oxydation continue
WO2003070632A1 (fr) * 2002-02-21 2003-08-28 Degussa Ag Procede de production de peroxyde d'hydrogene
CN105800563A (zh) * 2014-12-31 2016-07-27 湖南长岭石化科技开发有限公司 蒽醌法制过氧化氢的氧化萃取方法和生产过氧化氢的方法
CN105800564A (zh) * 2014-12-31 2016-07-27 湖南长岭石化科技开发有限公司 蒽醌法制过氧化氢的氧化方法和生产过氧化氢的方法
CN105800565A (zh) * 2014-12-31 2016-07-27 湖南长岭石化科技开发有限公司 蒽醌法制过氧化氢的氢化方法和生产过氧化氢的方法
CN105800562A (zh) * 2014-12-31 2016-07-27 湖南长岭石化科技开发有限公司 蒽醌法制过氧化氢的萃取方法和过氧化氢的制备方法

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19843573A1 (de) 1998-09-23 2000-03-30 Degussa Blasensäule und deren Verwendung
US7416718B2 (en) * 2005-08-31 2008-08-26 Fmc Corporation Auto-oxidation production of hydrogen peroxide via oxidation in a microreactor
JP2015020940A (ja) * 2013-07-22 2015-02-02 国立大学法人静岡大学 過酸化水素合成方法
SE541158C2 (en) * 2017-04-19 2019-04-16 Eb Nuberg Ab Oxidation column for hydrogen peroxide production

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE740674C (de) * 1939-07-05 1943-10-26 Ig Farbenindustrie Ag Durchfuehrung von Reaktionen zwischen Gasen und Fluessigkeiten
FR1097506A (fr) * 1953-04-01 1955-07-06 Pintsch Bamag Ag Procédé pour conduire de façon continue des réactions entre gaz et liquides
DE1212970B (de) * 1960-10-18 1966-03-24 Bombrini Parodi Delfino Societ Vorrichtung zur katalytischen Oxydation von organischen Verbindungen im fluessigen Zustand mit Sauerstoff
DE2003268A1 (de) * 1970-01-26 1971-07-29 Degussa Verfahren zur Herstellung von Wasserstoffperoxid
FR2228717A1 (en) * 1973-05-11 1974-12-06 Elektrokemiska Ab Continuous hydrogen peroxide prepn - by oxidising hydrogenated anthraquinone soln with gaseous oxygen

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4428923A (en) * 1982-11-09 1984-01-31 Degussa Aktiengesellschaft Continuous process for the production of hydrogen peroxide according to the anthraquinone process

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE740674C (de) * 1939-07-05 1943-10-26 Ig Farbenindustrie Ag Durchfuehrung von Reaktionen zwischen Gasen und Fluessigkeiten
FR1097506A (fr) * 1953-04-01 1955-07-06 Pintsch Bamag Ag Procédé pour conduire de façon continue des réactions entre gaz et liquides
DE1212970B (de) * 1960-10-18 1966-03-24 Bombrini Parodi Delfino Societ Vorrichtung zur katalytischen Oxydation von organischen Verbindungen im fluessigen Zustand mit Sauerstoff
DE2003268A1 (de) * 1970-01-26 1971-07-29 Degussa Verfahren zur Herstellung von Wasserstoffperoxid
FR2228717A1 (en) * 1973-05-11 1974-12-06 Elektrokemiska Ab Continuous hydrogen peroxide prepn - by oxidising hydrogenated anthraquinone soln with gaseous oxygen

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2652344A1 (fr) * 1989-09-22 1991-03-29 Kemira Oy Procede pour la production de peroxyde d'hydrogene.
FR2730987A1 (fr) * 1995-02-28 1996-08-30 Chemoxal Sa Installation de production d'eau oxygenee sur le site d'une papeterie
WO1996026895A1 (fr) * 1995-02-28 1996-09-06 Chemoxal S.A. Installation de production d'eau oxygenee sur le site d'une papeterie
CN1080699C (zh) * 1995-02-28 2002-03-13 凯默夏尔公司 在造纸厂生产过氧化氢的设备
US6756028B2 (en) 2000-10-21 2004-06-29 Degussa Ag Continuous hydrogenation process
WO2002034668A1 (fr) * 2000-10-21 2002-05-02 Degussa Ag Procede continu d'hydrogenation
US6861042B2 (en) 2000-10-21 2005-03-01 Degussa Ag Continuous hydrogenation process
EP1209122A1 (fr) * 2000-11-24 2002-05-29 Degussa AG Procédé d' oxydation continue
WO2002042202A1 (fr) * 2000-11-24 2002-05-30 Degussa Ag Procede d'oxydation continue
WO2003070632A1 (fr) * 2002-02-21 2003-08-28 Degussa Ag Procede de production de peroxyde d'hydrogene
US6982072B2 (en) 2002-02-21 2006-01-03 Degussa Ag Process for the production of hydrogen peroxide
KR100920318B1 (ko) * 2002-02-21 2009-10-07 에보니크 데구사 게엠베하 과산화수소의 제조방법
CN105800563A (zh) * 2014-12-31 2016-07-27 湖南长岭石化科技开发有限公司 蒽醌法制过氧化氢的氧化萃取方法和生产过氧化氢的方法
CN105800564A (zh) * 2014-12-31 2016-07-27 湖南长岭石化科技开发有限公司 蒽醌法制过氧化氢的氧化方法和生产过氧化氢的方法
CN105800565A (zh) * 2014-12-31 2016-07-27 湖南长岭石化科技开发有限公司 蒽醌法制过氧化氢的氢化方法和生产过氧化氢的方法
CN105800562A (zh) * 2014-12-31 2016-07-27 湖南长岭石化科技开发有限公司 蒽醌法制过氧化氢的萃取方法和过氧化氢的制备方法

Also Published As

Publication number Publication date
EP0221931A1 (fr) 1987-05-20
DE3666797D1 (en) 1989-12-14
JPS62502821A (ja) 1987-11-12
AU587257B2 (en) 1989-08-10
IN168293B (fr) 1991-03-09
ZA863259B (en) 1986-12-30
EP0221931B1 (fr) 1989-11-08
CA1283273C (fr) 1991-04-23
AU5868186A (en) 1986-12-04
ATE47819T1 (de) 1989-11-15
AR240549A1 (es) 1990-05-31

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